CN113480091A - SBBR sewage treatment device and method for removing phosphorus from side stream - Google Patents
SBBR sewage treatment device and method for removing phosphorus from side stream Download PDFInfo
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- 239000010865 sewage Substances 0.000 title claims abstract description 75
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 title claims abstract description 67
- 229910052698 phosphorus Inorganic materials 0.000 title claims abstract description 67
- 239000011574 phosphorus Substances 0.000 title claims abstract description 67
- 238000000034 method Methods 0.000 title claims abstract description 40
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 162
- 238000005273 aeration Methods 0.000 claims abstract description 76
- 239000010802 sludge Substances 0.000 claims abstract description 42
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 30
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 30
- 239000000701 coagulant Substances 0.000 claims abstract description 28
- 239000007788 liquid Substances 0.000 claims abstract description 16
- 239000006228 supernatant Substances 0.000 claims abstract description 15
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 14
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 14
- 239000001301 oxygen Substances 0.000 claims abstract description 14
- 238000010992 reflux Methods 0.000 claims abstract description 12
- 238000006243 chemical reaction Methods 0.000 claims description 99
- 239000007789 gas Substances 0.000 claims description 19
- 238000003756 stirring Methods 0.000 claims description 19
- 230000001105 regulatory effect Effects 0.000 claims description 15
- 230000001376 precipitating effect Effects 0.000 claims description 13
- 238000003860 storage Methods 0.000 claims description 12
- 230000008859 change Effects 0.000 claims description 7
- 230000000630 rising effect Effects 0.000 claims description 7
- 206010021143 Hypoxia Diseases 0.000 claims description 6
- 230000005484 gravity Effects 0.000 claims description 6
- 230000007954 hypoxia Effects 0.000 claims description 6
- 238000012544 monitoring process Methods 0.000 claims description 6
- 238000012545 processing Methods 0.000 claims description 6
- 238000001914 filtration Methods 0.000 claims description 3
- 230000007480 spreading Effects 0.000 claims description 3
- 238000003892 spreading Methods 0.000 claims description 3
- 230000003068 static effect Effects 0.000 claims description 3
- 238000004659 sterilization and disinfection Methods 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 230000035939 shock Effects 0.000 abstract description 3
- 230000008569 process Effects 0.000 description 26
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 22
- 244000005700 microbiome Species 0.000 description 13
- 229910052757 nitrogen Inorganic materials 0.000 description 11
- 241000894006 Bacteria Species 0.000 description 9
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 5
- 238000012163 sequencing technique Methods 0.000 description 4
- 238000007599 discharging Methods 0.000 description 3
- 230000036284 oxygen consumption Effects 0.000 description 3
- 238000004062 sedimentation Methods 0.000 description 3
- VMHLLURERBWHNL-UHFFFAOYSA-M Sodium acetate Chemical compound [Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 230000002354 daily effect Effects 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000003203 everyday effect Effects 0.000 description 2
- 238000001727 in vivo Methods 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 150000007524 organic acids Chemical class 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 2
- 235000017281 sodium acetate Nutrition 0.000 description 2
- 239000001632 sodium acetate Substances 0.000 description 2
- 229910019142 PO4 Inorganic materials 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- 230000008570 general process Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000006396 nitration reaction Methods 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 235000005985 organic acids Nutrition 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 125000001477 organic nitrogen group Chemical group 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/308—Biological phosphorus removal
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/06—Nutrients for stimulating the growth of microorganisms
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- Hydrology & Water Resources (AREA)
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- Water Supply & Treatment (AREA)
- Biodiversity & Conservation Biology (AREA)
- Organic Chemistry (AREA)
- Molecular Biology (AREA)
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- Activated Sludge Processes (AREA)
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Abstract
The invention discloses a SBBR sewage treatment device and method for removing phosphorus by side flow, the device comprises an SBBR reactor, the SBBR reactor is respectively connected with an adjusting tank and a sludge tank through pipelines, a supernatant reflux pump is also arranged between the sludge tank and the adjusting tank, the SBBR reactor is respectively connected with a first aeration fan and a second aeration fan through aeration pipes, a first water outlet pneumatic valve and a second water outlet pneumatic valve are arranged on the SBBR reactor, a liquid level sensor, a dissolved oxygen sensor and a temperature sensor are also arranged in the SBBR reactor, the SBBR reactor and the sludge tank are also connected with a coagulant adding device, and the SBBR reactor is connected with a carbon source adding device. The invention also comprises a method for treating sewage by adopting the device. The invention can improve the dephosphorization efficiency, and can effectively reduce the operation energy consumption and improve the shock load resistance of the system by accurately controlling various operation parameters through the feedback of the online temperature and the Do value by the PLC.
Description
Technical Field
The invention belongs to the technical field of sewage treatment, and particularly relates to a SBBR sewage treatment device and method for removing phosphorus from a side stream.
Background
With the development of ecological civilization construction in China, the treatment of water environment is continuously pushed to a new height, under increasingly strict environmental protection requirements, the sewage treatment water quality reaches the primary A discharge standard of pollutant discharge Standard of urban Sewage treatment plant (2002) and becomes the lowest discharge requirement gradually, indexes such as BOD5 and SS except nitrogen and phosphorus in sewage can be effectively removed under general process treatment, and the effective removal of nitrogen and phosphorus causing water eutrophication is difficult for various sewage treatment enterprises. The emission standard of nitrogen and phosphorus in the first-level A emission is as follows: the ammonia nitrogen is less than 5mg/L, the total nitrogen is less than 15mg/L, and the total phosphorus is less than 0.5 mg/L.
The biological denitrification process of sewage treatment mainly makes organic nitrogen undergo the processes of ammoniation, nitration and denitrification reaction to decompose and convert the nitrogen-containing organic matter in the waste water into N2And released to the atmosphere. The biological phosphorus removal process of sewage treatment mainly utilizes microorganisms such as phosphorus-accumulating bacteria and the like to release phosphorus under an anaerobic condition, then takes in excessive phosphorus under an aerobic condition, and then achieves the purpose of phosphorus removal by discharging residual sludge containing the phosphorus-accumulating bacteria. In the biological nitrogen and phosphorus removal process, enough carbon sources must be kept to maintain microorganisms to complete various reactions, but generally domestic sewage is too low in C/N ratio or carbon sources are difficult to reasonably distribute in each reaction stage, so that in all domestic sewage treatment enterprises, no matter AAO (anaerobic-anoxic-oxic) processes, MBR (Membrane bioreactor) processes, SBR (sequencing batch reactor) processes or other processes are adopted, carbon sources are basically required to be added for many times to promote biological reaction nitrogen removal, and flocculants are added for many times to remove phosphorus in the later treatment stage, so that the sewage treatment process is increased, and the operation cost and the sludge treatment capacity are greatly increased.
The SBBR sewage treatment process is from a SBR (sequencing batch reactor) sewage treatment process, and is characterized in that a solid medium for microorganism attachment is added into a reactor of the SBBR process, and the SBBR is a sequencing batch membrane bioreactor for short. In the SBBR technology, an aeration tank and a sedimentation tank are combined into a whole, five processes of water inlet, reaction (anaerobic, aerobic and anoxic), sedimentation, water outlet and idling are completed in the same reaction tank, one period is formed when one batch of water is treated, and after one period is completed, the next period is continued to be circulated in sequence. The SBBR process has the characteristics of small occupied area, strong impact load resistance, high degree of accurate automatic control, low energy consumption, stable effluent quality and the like. Although the removal rate of nitrogen and phosphorus in the SBBR sewage treatment process of the traditional operation procedure can generally reach 80%, the SBBR sewage treatment process is difficult to continuously reach the first-grade A discharge standard. Therefore, in order to enable the SBBR process to stably reach the 'first class A' emission standard, the operation process and the control method thereof need to be creatively changed.
Disclosure of Invention
Aiming at the defects, the invention provides the SBBR sewage treatment device and the method for removing phosphorus by side flow, which can improve the phosphorus removal efficiency, ensure that the water quality of effluent stably reaches the first-level A discharge standard, maximize the utilization rate of the added carbon source and coagulant, accurately control various operation parameters by PLC through the feedback of online temperature and Do value, effectively reduce the operation energy consumption and improve the shock load resistance of the system.
In order to achieve the purpose, the technical scheme adopted by the invention for solving the technical problems is as follows: the utility model provides a SBBR sewage treatment plant of sidestream dephosphorization, including the SBBR reactor, the SBBR reactor is connected with equalizing basin and sludge impoundment through the pipeline respectively, still be provided with the supernatant backwash pump between sludge impoundment and the equalizing basin, the SBBR reactor passes through the aeration pipe and is connected with aeration fan one and aeration fan two respectively, be provided with out water pneumatic valve one and play water pneumatic valve two on the SBBR reactor, and still be provided with level sensor in the SBBR reactor, dissolved oxygen sensor and temperature sensor, the supernatant backwash pump, level sensor, dissolved oxygen sensor and temperature sensor all are connected with controlling means, aeration fan one, aeration fan two and controlling means all with converter electric connection, it is connected with the sludge impoundment to go out the water pneumatic valve two other ends, SBBR reactor and sludge impoundment still are connected with the coagulant and add the device, be connected with the carbon source on the SBBR reactor and add the device.
Further, the coagulant adding device comprises a storage device filled with coagulant, and the storage device is connected with a coagulant adding metering pump.
Further, the carbon source adding device comprises a storage device filled with a carbon source, and the storage device is also connected with a carbon source adding metering pump.
Further, the control device is a PLC controller.
Further, a sewage pump is arranged in the adjusting tank and electrically connected with the control device.
The method for treating sewage by adopting the SBBR sewage treatment device for removing phosphorus from the side stream sequentially comprises the following steps of:
(1) stage of excessive phosphorus release
1) Water inflow: starting a sewage pump to feed water into the SBBR, stopping the sewage pump when the set water level H1 of the SBBR is reached, starting a carbon source addition metering pump while feeding water, and stopping when the set amount is reached;
2) anaerobic reaction: after water inflow stops, starting the second aeration fan to perform gas stirring at low frequency, intermittently operating the first aeration fan, stopping t2 every time t1 is operated, stopping reaction when the operation time reaches a set value t3, entering a standing and precipitating stage,
3) standing: the standing and precipitating time t4 is a set value;
4) water outlet: after standing, starting a water outlet pneumatic valve II, draining water in the reaction tank to a sludge tank by gravity, starting a coagulant addition metering pump t5 after the water outlet pneumatic valve II is started, wherein the flow rate of the metering pump is a set value, the addition amount of the coagulant is 800mg/L, and when the water level of the reaction tank reaches H3, closing the water outlet pneumatic valve II and the coagulant addition metering pump;
(2) secondary stage of phosphorus release
1) Water inflow: starting a sewage pump to feed water into the SBBR from the regulating reservoir, and stopping the sewage pump when the set water level H1 of the SBBR is reached;
2) anaerobic reaction: after water inflow stops, starting a second aeration fan to perform gas stirring at low frequency, intermittently operating the first aeration fan, stopping t2 every time t1 is operated, stopping reaction when the operation time reaches a set value t6, and entering an aerobic reaction stage;
3) aerobic reaction: starting a first aeration fan to carry out aeration, and monitoring an operation frequency P1 selected when a temperature sensor returns a temperature value in a T1 interval, an operation frequency P2 selected when the temperature is in a T2 interval and an operation frequency P3 selected when the temperature is in a T3 interval; when the Do value reaches 2mg/l and the change of the rising speed reaches a set value after a certain time t7, stopping the aerobic reaction at the moment of stopping the aeration fan, and entering an anoxic reaction stage;
4) and (3) hypoxia reaction: starting the second aeration fan to stir the gas, wherein the first aeration fan runs intermittently, the t9 is stopped when the t8 runs, the anoxic reaction is stopped when the running time reaches a set value t10, and the static stage is started;
5) standing: the standing and precipitating time t11 is a set value;
6) water outlet: after standing is finished, the water outlet pneumatic valve II is opened, water in the reaction tank is drained to a sludge tank by gravity, and the water outlet pneumatic valve II is closed when the water level of the reaction tank reaches H2;
(3) stage of official water outlet
1) Water inflow: starting a sewage pump to feed water into the SBBR, and stopping the sewage pump when the set water level H1 of the SBBR is reached;
2) anaerobic reaction: after water inflow stops, starting a second aeration fan to perform gas stirring at low frequency, intermittently operating the second aeration fan, stopping t2 every time t1 is operated, stopping reaction when the operation time reaches a set value t6, and entering an aerobic reaction stage;
3) aerobic reaction: starting a first aeration fan to carry out aeration, and monitoring an operation frequency P1 selected when a temperature sensor returns a temperature value in a T1 interval, an operation frequency P2 selected when the temperature is in a T2 interval and an operation frequency P3 selected when the temperature is in a T3 interval; when the Do value reaches 2mg/l, stopping the aeration fan and the aerobic reaction at a certain time t7 (when the change of the later rising speed reaches a set value), and entering an anoxic reaction stage;
4) and (3) hypoxia reaction: starting an aeration fan II to stir the gas, wherein the aeration fan I runs intermittently, stops t9 every time t8 is run, stops the anoxic reaction when the running time reaches a set value t10, and enters a standing stage;
5) standing: the standing and precipitating time t11 is a set value;
6) water outlet: after standing is finished, the first water outlet pneumatic valve is opened, water in the reaction tank enters the filter tank for filtration, then is subjected to disinfection treatment and then is discharged after reaching the standard, and the first water outlet pneumatic valve is closed when the water level of the reaction tank reaches H2;
step 1) to step 6) are the 1 st batch of water in the water outlet stage;
7) idling: when the liquid level meter of the regulating reservoir is detected to be at a low water level, the whole system enters an idle standby state;
8) when the liquid level of the regulating tank is at the normal water level, repeating the steps 1) to 6);
(4) and (4) repeating the steps (1) to (3) after the nth batch processing is finished.
Further, in the step (3), a batch of water can be treated every time the steps 1) to 6) are repeated, and n batches can be treated; during this period, in step 1) there are added: starting a supernatant reflux pump of the sludge tank to enter the regulating tank while starting the sewage pump, uniformly spreading the supernatant of the sludge tank into the water inlet of each batch when the water is fed from the 2 nd batch to the nth batch to empty the sludge tank, and determining the running time of the reflux pump according to the liquid level of the sludge tank and the processing batch n.
In the whole sewage treatment project, the following stages are provided:
and (3) excessive phosphorus release stage: the stage only has anaerobic reaction, and aims to decompose phosphorus-accumulating in vivo to release phosphate by microorganisms (phosphorus-accumulating bacteria (PAOs) mainly used as phosphorus-removing bacteria), add enough organic carbon source to increase C/N on one hand, and provide low-chain organic acid (VFAs) for the phosphorus-accumulating bacteria (PAOs) on the other hand to enable the phosphorus-accumulating bacteria to release the phosphorus-accumulating in vivo fully and excessively, wherein the phosphorus-releasing amount in water can reach about 30-40mg/L, sodium acetate is usually used as the carbon source, and the adding amount of general domestic sewage is usually 200mg/L (the adding value when the maximum phosphorus-releasing amount is reached during debugging). Two thirds of water (phosphorus-rich water) after sufficient excessive phosphorus release is discharged into a sludge tank, phosphorus is precipitated and removed by the action of a coagulant (PAC), and the addition amount of the coagulant (PAC) of general domestic sewage is usually 800 mg/L. In the stage, the small aeration fan performs gas stirring at low frequency and the large aeration fan performs gas stirring in an intermittent operation mode, and because the oxygen consumption of microorganisms is greater than the oxygen supply amount of the fan, a Do value oscillogram is in a sawtooth shape, but the highest Do value is controlled within 0.1 mg/L. As the water temperature is changed from 5 ℃ to 35 ℃ within one year, the oxygen demand of microorganisms is greatly different due to different temperatures, and different temperature intervals can be corresponding to different fan operation frequencies or different power fans to obtain different oxygen supply amounts, so that the requirements of various stages of the microorganisms are met, and the energy consumption is also saved.
(2) And (3) secondary phosphorus release stage: in this stage, after anaerobic, aerobic and anoxic reactions and standing (sedimentation), quarter of the water is discharged to a sludge tank. Because the last stage has no aerobic reaction, the growth of the phosphorus-accumulating bacteria is inhibited by excessive phosphorus release, the activity is gradually recovered until the aerobic reaction enters the stage, but the task of excessive phosphorus accumulation is not completed before the aerobic reaction is finished, the phosphorus content in the tail end water at the stage is 0.5-2mg/L, the excessive low-chain organic acids (VFAs) are possibly absorbed in the early stage of the phosphorus-accumulating bacteria and stored in the body in the form of poly-beta-hydroxyalkanoic acid (PHA), the stage of growth propagation and population optimization is positioned, the orthophosphate is absorbed by the phosphorus-accumulating bacteria (PAOs) at the subsequent aerobic stage to remove the phosphorus, the characteristic that the phosphorus release amount is more and more along with time is presented, and the foundation is laid for the water yielding of more than ten batches at the later stage.
The water yield of the stage is normal water yield, which accounts for one fourth of the effective volume of the reaction tank, and the drained water is also discharged into a sludge tank. In the stage, a small aeration fan is used for gas stirring in an anoxic reaction and a large aeration fan is used for gas stirring in an intermittent operation mode, a large fan is used for continuous aeration in an aerobic reaction, a control program also adopts different fan operation frequencies (or fans with different power configurations or fans with different quantity combinations to obtain different oxygen supply amounts) in different temperature intervals, the oxygen supply amount can meet the oxygen consumption of microorganisms during decomposition of organic matters and keep the Do value of 2mg/L in water, after the organic matters are gradually decomposed and absorbed by the microorganisms, the oxygen consumption of the microorganisms is reduced, the Do value in water is increased in an index curve form, and the aerobic reaction is finished when the rising rate reaches a set value.
(3) And (3) formal water outlet stage: the anaerobic reaction, the aerobic reaction and the anoxic reaction are basically the same as the previous stage, after the reaction is finished, standing (precipitating), yielding water, leaving unused, repeating the process for 16-20 batches, wherein the phosphorus-releasing floras greatly enhance the phosphorus-accumulating capacity due to excessive phosphorus release, the phosphorus content of 9 th and 10 th batches of water is even less than 0.1mg/L, then each batch of water slowly rises, and the reaction is finished when the water value is close to the set water value (0.5 mg/L). Due to different water qualities in different places and different batches which can be repeatedly processed, reasonable parameters need to be set in the debugging stage. In the treatment of each batch of water, the supernatant of the sludge pond is also split for treatment.
In summary, the invention has the following advantages:
1. the invention can improve the dephosphorization efficiency, ensure that the effluent quality stably reaches the first-class A discharge standard, maximize the utilization rate of the added carbon source and coagulant, and accurately control various operation parameters by PLC through the feedback of the online temperature and Do value, effectively reduce the operation energy consumption and improve the shock load resistance of the system.
2. The method depends on an SBBR sequencing batch sewage treatment process, the phosphorus removal mode of the traditional process is overturned, phosphorus removal is carried out in a mode of replacing microorganism phosphorus accumulation and sludge discharge with microorganism phosphorus release and drainage, the potential of microorganism phosphorus release is maximally excavated by reasonably adding a carbon source, and even the total phosphorus in effluent is controlled to be less than 0.3mg/L by a program, so that the reliability of system phosphorus removal is ensured; aiming at the temperature change in four seasons, the PLC selects different operating frequencies of the aeration fans for different temperature intervals, so that the stability of the system is improved, and the energy consumption is reduced.
3. The method has good biological phosphorus removal effect, can ensure that the total phosphorus of the effluent is less than or equal to 0.4mg/L, has strong controllability, and can further improve the quality of the effluent by adjusting control parameters. The biological phosphorus removal and sustainable and stable standard reaching are the biggest advantages of the invention. By adopting the side-stream phosphorus removal, the chemical phosphorus removal amount is reduced to the maximum extent, the dosage of a coagulant (PAC) is 40-50mg/L calculated by n batches of water in one-time side-stream phosphorus removal treatment, the dosage of a carbon source is reduced, and the dosage is usually 10-12.5mg/L when sodium acetate is used as the carbon source. Therefore, the using amount of chemical agents and carbon sources is reduced, the operation cost is reduced, and the sludge yield is greatly reduced.
4. The automation degree of the whole device operation process is high, the reaction efficiency (short reaction time, low energy consumption, low cost of medicaments such as carbon sources and the like) is improved by PLC accurate control, and unattended operation can be realized. The whole system has strong impact load resistance and extremely small mud production; and has the advantages of short process flow, small occupied area and small investment.
Drawings
FIG. 1 is a schematic diagram of an SBBR sewage treatment plant for sidestream phosphorus removal;
wherein, 1, SBBR reactor; 2. a regulating tank; 3. a sludge tank; 4. a sewage pump; 5. a water outlet pneumatic valve I; 6. a water outlet pneumatic valve II; 7. a first aeration fan; 8. a second aeration fan; 9. a carbon source adding metering pump; 10. a coagulant addition metering pump; 11. a supernatant reflux pump; 12. a liquid level sensor; 13. a dissolved oxygen sensor; 14. a temperature sensor; 15. a frequency converter; 16. a PLC controller; 17. an aeration pipe.
Detailed Description
The following detailed description of embodiments of the invention refers to the accompanying drawings.
In one embodiment of the present invention, as shown in fig. 1, an SBBR sewage treatment apparatus for removing phosphorus by side stream is provided, which includes an SBBR reactor 1, the SBBR reactor 1 is connected to an adjusting tank 2 and a sludge tank 3 through pipes, respectively, the adjusting tank 2 is provided with a sewage pump 4, the sewage pump 4 is electrically connected to a control device, a supernatant reflux pump 11 is further provided between the sludge tank 3 and the adjusting tank 2, the SBBR reactor 1 is connected to a first aeration blower 7 and a second aeration blower 8 through an aeration pipe 17, the SBBR reactor 1 is provided with a first water outlet pneumatic valve 5 and a second water outlet pneumatic valve 6, the SBBR reactor 1 is further provided with a liquid level sensor 12(AL200 piezoresistive liquid level transmitter), a dissolved oxygen sensor 13(InPro 6950i dissolved oxygen sensor) and a temperature sensor 14(TS418-1N 426), the supernatant reflux pump 11, the liquid level sensor 12, the dissolved oxygen sensor 13 and the temperature sensor 14 are all connected to the control device, the control device is ohm dragon CP1H-X40DT-D type PLC controller 16, aeration fan I7, aeration fan II 8 and control device are all electrically connected with frequency converter 15, the other end of water outlet pneumatic valve II 6 is connected with sludge impoundment 3, SBBR reactor 1 and sludge impoundment 3 are still connected with coagulant adding device, coagulant adding device is including the storage device who is equipped with the coagulant, storage device is connected with coagulant adding metering pump 10, be connected with carbon source adding device on the SBBR reactor 1, carbon source adding device is including the storage device who is equipped with the carbon source, storage device is still connected with carbon source adding metering pump 9.
The method for treating sewage by adopting the SBBR sewage treatment device for removing phosphorus from the side stream sequentially comprises the following steps of:
(1) stage of excessive phosphorus release
1) Water inflow: starting a sewage pump to feed water into the SBBR, stopping the sewage pump when the set water level H1 of the SBBR is reached, starting a carbon source addition metering pump while feeding water, and stopping when the set amount is reached;
2) anaerobic reaction: after water inflow stops, starting the second aeration fan to perform gas stirring at low frequency, intermittently operating the first aeration fan, stopping t2 every time t1 is operated, stopping reaction when the operation time reaches a set value t3, entering a standing and precipitating stage,
3) standing: the standing and precipitating time t4 is a set value;
4) water outlet: after standing, starting a water outlet pneumatic valve II, draining water in the reaction tank to a sludge tank by gravity, starting a coagulant addition metering pump t5 after the water outlet pneumatic valve II is started, wherein the flow rate of the metering pump is a set value, the addition amount of the coagulant is 800mg/L, and when the water level of the reaction tank reaches H3, closing the water outlet pneumatic valve II and the coagulant addition metering pump;
(2) secondary stage of phosphorus release
1) Water inflow: starting a sewage pump to feed water into the SBBR from the regulating reservoir, and stopping the sewage pump when the set water level H1 of the SBBR is reached;
2) anaerobic reaction: after water inflow stops, starting a second aeration fan to perform gas stirring at low frequency, intermittently operating the first aeration fan, stopping t2 every time t1 is operated, stopping reaction when the operation time reaches a set value t6, and entering an aerobic reaction stage;
3) aerobic reaction: starting a first aeration fan to carry out aeration, and monitoring an operation frequency P1 selected when a temperature sensor returns a temperature value in a T1 interval, an operation frequency P2 selected when the temperature is in a T2 interval and an operation frequency P3 selected when the temperature is in a T3 interval; when the Do value reaches 2mg/l and the change of the rising speed reaches a set value after a certain time t7, stopping the aerobic reaction at the moment of stopping the aeration fan, and entering an anoxic reaction stage;
4) and (3) hypoxia reaction: starting the second aeration fan to stir the gas, wherein the first aeration fan runs intermittently, the t9 is stopped when the t8 runs, the anoxic reaction is stopped when the running time reaches a set value t10, and the static stage is started;
5) standing: the standing and precipitating time t11 is a set value;
6) water outlet: after standing is finished, the water outlet pneumatic valve II is opened, water in the reaction tank is drained to a sludge tank by gravity, and the water outlet pneumatic valve II is closed when the water level of the reaction tank reaches H2;
(3) stage of official water outlet
1) Water inflow: starting a sewage pump to feed water into the SBBR, and stopping the sewage pump when the set water level H1 of the SBBR is reached;
2) anaerobic reaction: after water inflow stops, starting a second aeration fan to perform gas stirring at low frequency, intermittently operating the second aeration fan, stopping t2 every time t1 is operated, stopping reaction when the operation time reaches a set value t6, and entering an aerobic reaction stage;
3) aerobic reaction: starting a first aeration fan to carry out aeration, and monitoring an operation frequency P1 selected when a temperature sensor returns a temperature value in a T1 interval, an operation frequency P2 selected when the temperature is in a T2 interval and an operation frequency P3 selected when the temperature is in a T3 interval; when the Do value reaches 2mg/l, stopping the aeration fan and the aerobic reaction at a certain time t7 (when the change of the later rising speed reaches a set value), and entering an anoxic reaction stage;
4) and (3) hypoxia reaction: starting an aeration fan II to stir the gas, wherein the aeration fan I runs intermittently, stops t9 every time t8 is run, stops the anoxic reaction when the running time reaches a set value t10, and enters a standing stage;
5) standing: the standing and precipitating time t11 is a set value;
6) water outlet: after standing is finished, the first water outlet pneumatic valve is opened, water in the reaction tank enters the filter tank for filtration, then is subjected to disinfection treatment and then is discharged after reaching the standard, and the first water outlet pneumatic valve is closed when the water level of the reaction tank reaches H2;
step 1) to step 6) are the 1 st batch of water in the water outlet stage;
7) idling: when the liquid level meter of the regulating reservoir is detected to be at a low water level, the whole system enters an idle standby state;
8) when the liquid level of the regulating tank is at the normal water level, repeating the steps 1) to 6), and treating a batch of water once every time repeating the steps 1) to 6), wherein n batches of water can be treated in a set manner; during this period, in step 1) there are added: starting a supernatant reflux pump of the sludge tank to enter the regulating tank while starting the sewage pump, uniformly spreading the supernatant of the sludge tank into the water inlet of each batch when the water is fed from the 2 nd batch to the nth batch to empty the sludge tank, and determining the running time of the reflux pump according to the liquid level of the sludge tank and the processing batch n;
(4) and (4) repeating the steps (1) to (3) after the nth batch processing is finished.
The invention can be widely used for the treatment of distributed domestic sewage, is suitable for the upgrading and reconstruction of sewage treatment plants (stations) similar to SBR process, not only ensures the effluent quality, but also greatly saves the cost of medicaments and carbon sources.
In a specific implementation case, SBBR sewage treatment equipment adopting the process is arranged at a municipal discharge outlet of sewage in Ningxia certain holiday village, water is directly taken from a sewage well to an adjusting tank, the adjusting tank is lifted to a reaction tank through a lifting pump for treatment, and the quality of raw sewage is as follows: COD 310 + 515mg/L, total nitrogen 50-75mg/L, ammonia nitrogen 55-81mg/L, total phosphorus 6.1-9.2 mg/L. The effective volume of the reaction tank is 18m34.5m of water is discharged from each batch34-5 batches of water are discharged every day, and the daily average treatment capacity is 20m3And 8, discharging 16-20 batches of water formally after each phosphorus release, wherein the effluent quality COD is 30-40mg/L, the total nitrogen is less than 15mg/L, the ammonia nitrogen is less than 3mg/L, and the total phosphorus is less than 0.3 mg/L. The treated water is completely discharged into a municipal pipe network.
In another embodiment, a certain city administrative center office building is provided with a sewage treatment device adopting the SBBR process, water is directly taken from a last-stage septic tank to a reaction tank, sewage in the reaction tank is lifted to the reaction tank for treatment, and the quality of raw sewage is as follows: 210-360mg/L of COD, 76-81mg/L of total nitrogen, 55-70mg/L of ammonia nitrogen and 6-7mg/L of total phosphorus. Effective volume of reaction tank is 92m3Each batch of water is discharged by 23m34-5 batches of water are discharged every day, and the daily average treatment capacity is 100m3And 8, discharging 16-20 batches of water regularly every time the phosphorus is released excessively, wherein the effluent quality COD is 30-40mg/L, the total nitrogen is less than 15mg/L, the ammonia nitrogen is less than 3mg/L, and the total phosphorus is less than 0.3 mg/L. Each office buildingThe sewage in 3-11 months of the year is completely treated and used for greening.
While the present invention has been described in detail with reference to the illustrated embodiments, it should not be construed as limited to the scope of the present patent. Various modifications and changes may be made by those skilled in the art without inventive step within the scope of the appended claims.
Claims (7)
1. The SBBR sewage treatment device for removing phosphorus by side flow is characterized by comprising an SBBR reactor, wherein the SBBR reactor is respectively connected with a regulating tank and a sludge tank through pipelines, a supernatant reflux pump is further arranged between the sludge tank and the regulating tank, the SBBR reactor is respectively connected with a first aeration fan and a second aeration fan through aeration pipes, the SBBR reactor is provided with a first water outlet pneumatic valve and a second water outlet pneumatic valve, a liquid level sensor, a dissolved oxygen sensor and a temperature sensor are further arranged in the SBBR reactor, the supernatant reflux pump, the liquid level sensor, the dissolved oxygen sensor and the temperature sensor are all connected with a control device, the first aeration fan, the second aeration fan and the control device are all electrically connected with a frequency converter, the other end of the second water outlet pneumatic valve is connected with the sludge tank, the SBBR reactor and the sludge tank are further connected with a coagulant adding device, and the SBBR is connected with a carbon source adding device.
2. The SBBR sewage treatment plant for sidestream phosphorus removal of claim 1, wherein said coagulant addition device comprises a storage device filled with coagulant, said storage device being connected with a coagulant addition metering pump.
3. The SBBR sewage treatment plant for sidestream phosphorus removal of claim 1, wherein said carbon source adding means comprises a storage device containing a carbon source, said storage device further connected to a carbon source adding metering pump.
4. The SBBR sewage treatment plant of sidestream phosphorus removal of claim 1, wherein said control device is a PLC controller.
5. The SBBR sewage treatment plant for sidestream phosphorus removal of claim 1, wherein a sewage pump is disposed in said surge tank, and said sewage pump is electrically connected to said control device.
6. The method for sewage treatment by adopting the SBBR sewage treatment plant for sidestream phosphorus removal of any one of claims 1-5, is characterized by comprising the following steps in sequence:
(1) stage of excessive phosphorus release
1) Water inflow: starting a sewage pump to feed water into the SBBR, stopping the sewage pump when the set water level H1 of the SBBR is reached, starting a carbon source addition metering pump while feeding water, and stopping when the set amount is reached;
2) anaerobic reaction: after water inflow stops, starting the second aeration fan to perform gas stirring at low frequency, intermittently operating the first aeration fan, stopping t2 every time t1 is operated, stopping reaction when the operation time reaches a set value t3, entering a standing and precipitating stage,
3) standing: the standing and precipitating time t4 is a set value;
4) water outlet: after standing, starting a water outlet pneumatic valve II, draining water in the reaction tank to a sludge tank by gravity, starting a coagulant addition metering pump t5 after the water outlet pneumatic valve II is started, wherein the flow rate of the metering pump is a set value, the addition amount of the coagulant is 800mg/L, and when the water level of the reaction tank reaches H3, closing the water outlet pneumatic valve II and the coagulant addition metering pump;
(2) secondary stage of phosphorus release
1) Water inflow: starting a sewage pump to feed water into the SBBR from the regulating reservoir, and stopping the sewage pump when the set water level H1 of the SBBR is reached;
2) anaerobic reaction: after water inflow stops, starting a second aeration fan to perform gas stirring at low frequency, intermittently operating the first aeration fan, stopping t2 every time t1 is operated, stopping reaction when the operation time reaches a set value t6, and entering an aerobic reaction stage;
3) aerobic reaction: starting a first aeration fan to carry out aeration, and monitoring an operation frequency P1 selected when a temperature sensor returns a temperature value in a T1 interval, an operation frequency P2 selected when the temperature is in a T2 interval and an operation frequency P3 selected when the temperature is in a T3 interval; when the Do value reaches 2mg/l and the change of the rising speed reaches a set value after a certain time t7, stopping the aerobic reaction at the moment of stopping the aeration fan, and entering an anoxic reaction stage;
4) and (3) hypoxia reaction: starting the second aeration fan to stir the gas, wherein the first aeration fan runs intermittently, the t9 is stopped when the t8 runs, the anoxic reaction is stopped when the running time reaches a set value t10, and the static stage is started;
5) standing: the standing and precipitating time t11 is a set value;
6) water outlet: after standing is finished, the water outlet pneumatic valve II is opened, water in the reaction tank is drained to a sludge tank by gravity, and the water outlet pneumatic valve II is closed when the water level of the reaction tank reaches H2;
(3) stage of official water outlet
1) Water inflow: starting a sewage pump to feed water into the SBBR, and stopping the sewage pump when the set water level H1 of the SBBR is reached;
2) anaerobic reaction: after water inflow stops, starting a second aeration fan to perform gas stirring at low frequency, intermittently operating the second aeration fan, stopping t2 every time t1 is operated, stopping reaction when the operation time reaches a set value t6, and entering an aerobic reaction stage;
3) aerobic reaction: starting a first aeration fan to carry out aeration, and monitoring an operation frequency P1 selected when a temperature sensor returns a temperature value in a T1 interval, an operation frequency P2 selected when the temperature is in a T2 interval and an operation frequency P3 selected when the temperature is in a T3 interval; when the Do value reaches 2mg/l, stopping the aeration fan and the aerobic reaction at a certain time t7 (when the change of the later rising speed reaches a set value), and entering an anoxic reaction stage;
4) and (3) hypoxia reaction: starting an aeration fan II to stir the gas, wherein the aeration fan I runs intermittently, stops t9 every time t8 is run, stops the anoxic reaction when the running time reaches a set value t10, and enters a standing stage;
5) standing: the standing and precipitating time t11 is a set value;
6) water outlet: after standing is finished, the first water outlet pneumatic valve is opened, water in the reaction tank enters the filter tank for filtration, then is subjected to disinfection treatment and then is discharged after reaching the standard, and the first water outlet pneumatic valve is closed when the water level of the reaction tank reaches H2;
step 1) to step 6) are the 1 st batch of water in the water outlet stage;
7) idling: when the liquid level meter of the regulating reservoir is detected to be at a low water level, the whole system enters an idle standby state;
8) when the liquid level of the regulating tank is at the normal water level, repeating the steps 1) to 6);
(4) and (4) repeating the steps (1) to (3) after the nth batch processing is finished.
7. The method according to claim 6, wherein in the step (3), a batch of water can be treated every time the steps 1) to 6) are repeated, and n batches can be treated; during this period, in step 1) there are added: starting a supernatant reflux pump of the sludge tank to enter the regulating tank while starting the sewage pump, uniformly spreading the supernatant of the sludge tank into the water inlet of each batch when the water is fed from the 2 nd batch to the nth batch to empty the sludge tank, and determining the running time of the reflux pump according to the liquid level of the sludge tank and the processing batch n.
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